Classifications

• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
  • C08J3/00—Processes of treating or compounding macromolecular substances
  • C08J3/12—Powdering or granulating
  • C08J3/124—Treatment for improving the free-flowing characteristics
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
  • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
  • B29B7/00—Mixing; Kneading
  • B29B7/002—Methods
  • B29B7/007—Methods for continuous mixing
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
  • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
  • B29B7/00—Mixing; Kneading
  • B29B7/74—Mixing; Kneading using other mixers or combinations of mixers, e.g. of dissimilar mixers ; Plant
  • B29B7/7476—Systems, i.e. flow charts or diagrams; Plants
  • B29B7/7495—Systems, i.e. flow charts or diagrams; Plants for mixing rubber
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
  • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
  • B29B9/00—Making granules
  • B29B9/02—Making granules by dividing preformed material
  • B29B9/06—Making granules by dividing preformed material in the form of filamentary material, e.g. combined with extrusion
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
  • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
  • B29B9/00—Making granules
  • B29B9/12—Making granules characterised by structure or composition
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
  • C08J3/00—Processes of treating or compounding macromolecular substances
  • C08J3/005—Processes for mixing polymers
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
  • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
  • B29B7/00—Mixing; Kneading
  • B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices
  • B29B7/34—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices
  • B29B7/38—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
  • C08J2321/00—Characterised by the use of unspecified rubbers

Definitions

• agglomeration problem associated with pellets of rubbery polymers is sometimes overcome by coating the pellets with a fused resinous partitioning agent, such as polystyrene, polymethylmethacrylate, polyacrylonitrile, polyvinylchloride (PVC) or polyethylene.
• a fused resinous partitioning agent such as polystyrene, polymethylmethacrylate, polyacrylonitrile, polyvinylchloride (PVC) or polyethylene.
• PVC polyvinylchloride
• United States Patent 3,813,259 refers to the use of polymethylmethacrylate as a partitioning agent
• United States Patent 4,271,213 described the use of a mixture of styrene-butadiene copolymer resin and polymethylmethacrylate resin as a partitioning agent.
• inorganic partitioning agents such as talc
• talc inorganic partitioning agents
• dry powders tend to settle out during coating applications which lead to undesirable inconsistencies.
• inorganic or polymeric partitioning agents cannot be tolerated.
• the presence of talc cannot be tolerated in nitrile rubber used to make electrical cable because it can interfere with useful functional service life.
• free-flowing crumb compositions can easily be made on a commercial basis.
• the technique of this invention also eliminates the need to utilize inorganic or polymeric partitioning agents in free-flowing crumb rubber compositions.
• the subject invention more specifically discloses a process for preparing a free-flowing crumb rubber composition which comprises the steps of:
• the subject invention further discloses a process for preparing a free-flowing crumb rubber composition which comprises the steps of:
• the present invention also reveals a free-flowing crumb rubber composition which is comprised of pellets of a rubbery polymer having a diameter which is within the range of about 1 mm to about 15 mm, wherein the surface of the pellets of rubbery polymer is coated with a wax having a melting point which is within the range of about 40°C to about 175°C, and wherein the free-flowing crumb rubber composition contains from about 1 weight percent to about 10 weight percent of the wax.
• the techniques of this invention can be used to make a free-flowing crumb of virtually any type of rubbery polymer. This can be accomplished by using an extrusion technique or a coagulation technique.
• the rubbery polymer will be comprised of repeat units which are derived from one or more conjugated diolefin monomers, such as 1,3-butadiene or isoprene. It can also contain repeat units which are derived from one or more monomers which are copolymerizable with the conjugated diolefin monomer, such as acrylonitrile, styrene, ⁇ -methylstyrene or n-butylacrylate.
• rubbery polymers which can be used include: polybutadiene rubber, polyisoprene rubber, styrene-butadiene rubber (SBR), styrene-isoprene rubber (SIR), isoprene-butadiene rubber (IBR), styrene-isoprene-butadiene rubber (SIBR), nitrile rubber (NBR) or carboxylated nitrile rubber.
• the rubbery polymer is extruded into pellets. It is, of course, necessary to have previously processed the rubber into a physical form that can be fed into an extruded. For instance, bailed rubber could be processed through a Banbury mixer to put it into a physical form which can be fed into an extruder. It is important for the extruder to be operated at a speed in a manner whereby the rubber exiting the extruder is at a temperature of less than about 150°C.
• the temperature profile of the extruder should use temperature ranges which will allow the extrudate to be maintained at the desired temperatures. A typical temperature profile might include temperatures within the range of 100°C to 150°C.
• the rubber exiting the extruder will typically be at a temperature of less than about 125°C.
• the rubber will be extruded into pellets which have a diameter which is within the range of about 1 mm (millimeter) to about 15 mm.
• the rubber will typically be extruded into pellets having a diameter which is within the range of about 2 mm to about 10 mm.
• the pellets will preferably have a diameter of 4 mm to 6 mm.
• the pellets extruded are typically cut to a length of about 1 mm to about 15 mm.
• the pellets will more typically be cut to a length of about 2 mm to 10 mm and will preferably be cut to a length of about 2 mm to 6 mm.
• the pellets of rubbery polymer are extruded into a wax emulsion.
• the wax emulsion is maintained at a temperature which is within the range of about 5°C to about 70°C. It is normally preferred for the wax emulsion to be at a temperature which is within the range of about 20°C to about 50°C. However, it is critical for the temperature of the wax emulsion to be maintained at a temperature which is less than the melting point of the wax being employed.
• the wax emulsion is comprised of water, the wax and an emulsifier. It will typically contain from about 35 weight percent to about 89 weight percent water, from about 10 weight percent to about 50 weight percent of the wax, and from about 1 weight percent to about 15 weight percent of the emulsifier.
• the wax emulsion will preferably contain from about 62 weight percent to about 83 weight percent water, from about 15 weight percent to about 30 weight percent of the wax, and from about 2 weight percent to about 8 weight percent of the emulsifier.
• the wax emulsion will preferably contain from about 69 weight percent to about 76 weight percent water, from about 20 weight percent to about 25 weight percent of the wax, and from about 4 weight percent to about 6 weight percent of the emulsifier.
• the wax will have a melting point which is within the range of about 40°C to about 175°C. It will preferably have a melting point which is within the range of about 50°C to about 150°C and will most preferably have a melting point which is within the range of about 60°C to about 70°C.
• the wax is an ester of a high molecular weight fatty acid with a high molecular weight alcohol other than glycerol. It will typically be a mineral wax selected from the group consisting of paraffin waxes, microcrystalline waxes, oxidized microcrystalline waxes, montan waxes, hoechst waxes and ozokerite waxes. Paraffin waxes are normally preferred.
• the emulsifier can be virtually any type of anionic emulsifier or nonionic emulsifier.
• anionic surfactants which can be utilized include carboxylates, alkylbenzene sulfonates, alkane sulfonates, ⁇ -olefin sulfonates, fatty alcohol sulfates and oxo-alcohol sulfates.
• alkyl benzene sulfonates fatty alcohol sulfates and oxo-alcohol ether sulfates are preferred.
• the emulsifier is generally preferred for the emulsifier to be a nonionic emulsifier.
• nonionic surfactants include alkylphenol ethoxylates, fatty-alcohol polyethyleneglycol ethers, oxo-alcohol polyethyleneglycol ethers, ethylene oxide polymers, propylene oxide polymers and fatty alcohol polyglycol ethers.
• Ethoxylated alcohols are a highly preferred class of nonionic emulsifiers.
• the wax emulsion containing the rubbery polymer will be agitated so as to thoroughly mix the wax and the rubbery polymer pellets together. This mixing allows for the wax to coat the surface of the rubbery polymer. During this mixing step, the rubbery polymer will by coated with about 1 weight percent to about 10 weight percent wax, based upon the total weight of the wax-coated rubbery polymer pellets. More typically, the rubbery polymer will be coated with about 2 weight percent to about 5 weight percent of the wax.
• the wax-coated rubbery polymer pellets are then separated from the wax emulsion. This can be done by simply pouring the wax emulsion containing the rubbery polymer through a screen which is small enough to catch the rubbery pellets. The removal of the wax emulsion from the wax-coated rubbery pellets can be facilitated by centrifugation.
• the wet wax-coated rubbery pellets which are recovered from the wax emulsion generally contain less than about 2 percent water. These wet pellets are then dried to further reduce the level of water present to less than about 0.5 percent. It is highly preferred for this drying step to be carried out under forced motion.
• the forced motion must be sufficient to keep the wax-coated rubbery polymer pellets from agglomerating prior to being dried.
• the drying will typically be accomplished by passing a gas medium through a bed of the wax-coated rubbery polymer pellets.
• the forced motion is provided by passing the gas medium through the bed of wax-coated rubbery polymer pellets at a velocity which is sufficient to fluidize the bed of wax-coated rubbery polymer pellets.
• the drying temperature employed will typically be within the range of about 10°C to about 50°C. It is normally preferred to utilize a drying temperature which is within the range of about 20°C to about 40°C.
• the drying temperatures referred to herein are the temperatures of the gas medium used in the drying step.
• the gas medium utilized will typically be air. However, other gases such as nitrogen can also be utilized. It is generally advantageous for the gas medium to be dried and heated prior to utilization in the drying step.
• the free-flowing crumb rubber composition made by this process is comprised of pellets of a rubbery polymer having a diameter which is within the range of about 1 mm to about 15 mm, wherein the surface of the pellets of rubbery polymer is coated with a wax having a melting point which is within the range of about 40°C to about 175°C, and wherein the free-flowing crumb rubber composition contains from about 1 weight percent to about 10 weight percent of the wax.
• This free-flowing crumb rubber composition is free of inorganic materials and polymeric materials other than the rubbery polymer itself.
• These free-flowing crumb rubber compositions should be stored at a temperature of less than about 60°F (16°) to prevent agglomerating from occurring.
• the free-flowing crumb rubber composition will preferably be stored at a temperature of less than 40°F (4°C).
• a wax emulsion is added to a latex of a rubbery polymer. This can be accomplished by simply adding the wax emulsion to the latex.
• the amount of wax emulsion added will normally be sufficient to contain from about 1 weight percent to about 10 weight percent wax, based upon the dry weight of the rubbery polymer in the latex.
• the amount of wax emulsion added will preferably be sufficient to contain from about 2 weight percent to about 5 weight percent wax, based upon the dry weight of the rubbery polymer in the latex.
• the wax containing latex will be agitated so as to thoroughly mix the wax emulsion into the latex.
• This mixing step is normally carried out at a temperature which is within the range of about 5°C to about 70°C. It is normally preferred for the mixing to be done while the latex is at a temperature which is within the range of about 20°C to about 50°C. In any case, it is critical for the temperature of the latex to be maintained at a temperature which is less than the melting point of the wax being employed.
• the wax emulsion is comprised of water, the wax and an emulsifier.
• the wax will have a melting point which is within the range of about 40°C to about 175°C. It will preferably have a melting point which is within the range of about 50°C to about 150°C and will most preferably have a melting point which is within the range of about 60°C to about 70°C.
• the wax is an ester of a high molecular weight fatty acid with a high molecular weight alcohol other than glycerol. It will typically be a mineral wax selected from the group consisting of paraffin waxes, microcrystalline waxes, oxidized microcrystalline waxes, montan waxes, hoechst waxes and ozokerite waxes. Paraffin waxes are normally preferred.
• the emulsifier can be virtually any type of anionic emulsifier or nonionic emulsifier.
• anionic surfactants which can be utilized include carboxylates, alkylbenzene sulfonates, alkane sulfonates, ⁇ -olefin sulfonates, fatty alcohol sulfates and oxo-alcohol sulfates.
• alkyl benzene sulfonates fatty alcohol sulfates and oxo-alcohol ether sulfates are preferred.
• the emulsifier is generally preferred for the emulsifier to be a nonionic emulsifier.
• nonionic surfactants include alkylphenol ethoxylates, fatty-alcohol polyethyleneglycol ethers, oxo-alcohol polyethyleneglycol ethers, ethylene oxide polymers, propylene oxide polymers and fatty alcohol polyglycol ethers.
• Ethoxylated alcohols are a highly preferred class of nonionic emulsifiers.
• the latex which contains the wax is coagulated.
• the latex which contains the wax can be coagulated using a conventional salt/acid coagulation procedure.
• a combination of a salt and an acid can be added to the latex to cause coagulation.
• Such salt/acid coagulation is typically accomplished by simply adding at least one strong inorganic acid and a salt to the latex.
• Coagulation aids can also be employed in coagulation of the rubbery polymer containing emulsion.
• Some representative examples of strong inorganic acids which can be used in the coagulation of latex include sulfuric acid, hydrochloric acid and nitric acid with sulfuric acid being preferred.
• a wide variety of salts can be employed. Some representative examples of salts which can be used include sodium chloride, potassium chloride, calcium chloride, aluminum sulfate, magnesium sulfate and quaternary ammonium salts. The amount of salt and acid needed to cause coagulation will vary with the specific emulsion and with the type of salt utilized. Calcium chloride is a highly preferred salt and will normally be added in an amount which is within the range of about 13 phr to about 40 phr.
• a coagulated rubber slurry is formed.
• the rubber in the slurry is in the form of wax-coated crumb rubber.
• the coagulated rubber slurry is comprised of serum and the wax-coated rubber crumb.
• the serum is essentially the aqueous phase with the rubber crumb being the solid phase.
• the serum is, of course, comprised of water, emulsifier, acids, salts and other water-soluble residual compounds.
• the coagulated rubber slurry is typically transferred to a conversion tank in order to complete the coagulation process.
• the wax-coated rubber crumb is then filtered through a shaker screen which collects the wax-coated rubber crumb and deposits it within a reslurry tank. Washing is typically employed to remove excess soap and/or electrolyte from the wax-coated crumb rubber.
• the wax-coated rubber crumb is washed and agitated in fresh wash water to produce a wax-coated rubber reslurry.
• the pH of the rubber reslurry can then optionally be adjusted so as to be within the range of about 5 to about 8.
• This neutralization step is accomplished by the addition of a base.
• bases known to those of skill in the art may be utilized, including calcium hydroxide, magnesium hydroxide, potassium hydroxide and sodium hydroxide.
• the pH of the wax-coated rubber reslurry will preferably be adjusted to be within the range of about 5.5 to about 7.5 and will most preferably be adjusted to be within the range of about 6 to about 7.
• the serum from the shaker screen is then typically recycled back to the coagulator, permitting efficient use of the coagulants.
• the wax-coated rubber crumb from the reslurry tank then normally passes over a second shaker screen and is directed to an expeller, in which the polymer can be dewatered.
• the expeller typically consists of a screw which transports the rubber down a shaft of the expeller under increasingly constricting conditions.
• the barrel of the expeller is lined lengthwise with narrow grooves, the width of which decreases as the rubber moves through the expeller.
• the water can optionally be squeezed out through the grooves while the rubber advances to an open-ended cone located at the far end of the barrel.
• the cone provides a back-pressure for the dewatering screw.
• the dewatering force can be controlled by adjusting the setting of the cone. This adjustment can vary with different types of rubber and can be altered during a finishing run to attain the desired moisture content.
• the moisture content of the rubber exiting the expeller is typically about 10 weight percent.
• the dewatered wax-coated rubber is then typically dried. It is highly preferred for this drying step to be carried out under forced motion.
• the forced motion must be sufficient to keep the wax-coated crumb rubber from agglomerating prior to being dried.
• the drying will typically be accomplished by passing hot air through a bed of the wax-coated crumb rubber.
• the forced motion is provided by passing the hot air medium through the bed of wax-coated rubbery polymer particles at a velocity which is sufficient to fluidize the bed of wax-coated rubbery polymer particles.
• Higher drying temperatures promote faster drying which, of course, reduces the time needed for drying. However, high temperatures can lead to polymer degradation and agglomeration which limits the drying temperature which can be utilized.
• the maximum drying temperature is limited to a maximum of about 210°F (99°C) because the heat history of the rubber significantly affects ultimate properties. Drying temperatures as low as room temperature (about 20°C) can be employed. However, in order to attain a commercially satisfactory drying rate, the temperature will normally be at least about 150°F (66°C). Thus, the drying temperature employed will typically be within the range of about 150°F (66°C) to about 210°F (99°C). It is normally preferred to utilize a drying temperature which is within the range of about 165°F (74°C) to about 195°F (91°C).
• the wax-coated crumb rubber is air-conveyed to a cyclone, where it subsequently falls onto a metal apron and proceeds through an apron drier.
• the cyclone functions as a knock-out vessel that separates the rubber from the air. Consequently, the rubber falls onto the apron in a uniform, dispersed manner.
• the apron drier is typically a single-pass drier containing a series of heated zones which may each be set to specified temperatures. Hot air is directed through each zone at the specified temperature and removes the moisture from the wax-coated rubber. Both the zone temperatures and the apron speed may be varied to adjust the drying conditions within the apron dryer.
• the moisture content of the finished rubber is preferably less than about 1 percent, and more preferably below about 0.7 percent. When the rubber exits the apron dryer, it is allowed to cool and is packaged for shipping.
• the free-flowing crumb rubber composition made by this process is coated on its surface with a wax having a melting point which is within the range of about 40°C to about 175°C, wherein the free-flowing crumb rubber composition contains from about 1 weight percent to about 10 weight percent of the wax.
• This free-flowing crumb rubber composition is free of inorganic materials and polymeric materials other than the rubbery polymer itself.
• These free-flowing crumb rubber compositions should be stored at a temperature of less than about 60°F (16°) to prevent agglomerating from occurring. It is desirable to store the free-flowing crumb rubber composition at a temperature which is no greater than about 75°F (24°C). It is preferable to store the free-flowing crumb rubber at a temperature of less than 40°F (4°C). However, it is possible to store the free-flowing crumb rubber at higher temperatures for short periods without agglomeration.
• nitrile rubber crumb was prepared by utilizing the technique of this invention.
• 125 pounds (56.7 kg) of Chemigum® N615B nitrile rubber from The Goodyear Tire & Rubber Company was fed into a #4 Banbury mixer and was mixed for about 2 to 5 minutes.
• This nitrile rubber contained about 33 percent bound acrylonitrile.
• This mixing step was conducted in a manner whereby the final mixing temperature was kept below about 300°F (149°C).
• the nitrile rubber was then fed into an extruder-pelletizer and was extruded at a rate of 2500 pounds per hour (1134 kg/hour) through a multihole die.
• the die holes had a diameter of one-eighth inch (3 mm).
• the nitrile rubber being extruded was pelletized into an aqueous wax emulsion.
• the aqueous wax emulsion was made by diluting 100 parts of Petrolite® 01 dispersion with 100 parts of water.
• the aqueous wax emulsion contained 22.5 weight percent of a paraffin wax having a melting point of 64°C, 2.5 percent of an ethoxylated alcohol, and 75 weight percent water.
• the temperature of the wax emulsion was controlled to stay below 50°C and was agitated to mix the nitrile rubber pellets throughout the wax emulsion.
• the wax emulsion containing the nitrile rubber pellets was then fed into a centrifugal dryer which reduced the water content of the nitrile rubber pellets to less than 2 percent.
• the nitrile rubber pellets were then dried in a ribbon blender at a temperature of 100°F (38°C) to further reduce the moisture content of the nitrile rubber pellets which were then packaged in 50-pound (22.7 kg) boxes for storage and subsequent utilization.
• the crumb rubber composition made remained free-flowing after several months of storage in refrigeration at a temperature of less than 40°C (4°C).
• a free-flowing nitrile rubber crumb was prepared utilizing a wax having a melting point of 138°C.
• 125 pounds (56.7 kg) of Chemigum® N615B nitrile rubber from The Goodyear Tire & Rubber Company was fed into a #4 Banbury mixer and was mixed for about 2 to 5 minutes.
• This nitrile rubber contained about 33 percent bound acrylonitrile.
• This mixing step was conducted in a manner whereby the final mixing temperature was kept below about 300°F (149°C).
• the nitrile rubber was then fed into an extruder-pelletizer and was extruded at a rate of 2500 pounds per hour (1134 kg/hour) through a multihole die.
• the die holes had a diameter of one-eighth inch (3 mm).
• the nitrile rubber being extruded was pelletized into an aqueous wax emulsion.
• the aqueous wax emulsion contained 20 weight percent of a paraffin wax having a melting point of 138°C, 2 weight percent of an ethoxylated alcohol, and 78 weight percent water.
• the temperature of the wax emulsion was controlled to stay below 50°C and was agitated to mix the nitrile rubber pellets throughout the wax emulsion.
• the wax emulsion containing the nitrile rubber pellets was then fed into a centrifugal dryer which reduced the water content of the nitrile rubber pellets to less than 2 percent.
• the nitrile rubber pellets were then dried in a ribbon blender at a temperature of 100°F (38°C) to further reduce the moisture content of the nitrile rubber pellets which were then packaged in 50-pound (22.7 kg) boxes for storage and subsequent utilization.
• the crumb rubber composition made remained free-flowing after several months of storage in refrigeration at a temperature of less than 40°C (4°C).
• nitrile rubber crumb was prepared by utilizing the technique of this invention.
• 35 pounds (15.9 kg) of Chemigum® N615B nitrile rubber latex from The Goodyear Tire & Rubber Company was mixed with about 1 pound (0.454 kg) of Petrolite® 01 wax dispersion. This nitrile rubber contained about 33 percent bound acrylonitrile.
• the latex was then coagulated by the addition of 20 pounds (9.1 kg) of coagulant which was comprised of water and 240 grams of aluminum sulfate. The coagulation was carried out at a temperature of 160°F (71°C). After coagulation, the wax-coated crumb rubber was twice washed with 20 gallons (76 liters) of cold tap water. The crumb rubber was then dried on a fine screen at a temperature of 120°F (49°C) which reduced the water content of the nitrile rubber crumb to less than 0.5 percent. The crumb rubber composition made remained free-flowing after several months of storage at room temperature (about 20°C).

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• 1997
  • 1997-04-02 EP EP97105485A patent/EP0801093A3/fr not_active Withdrawn
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